CN105833804A - Steam rising type radial-flow reactor - Google Patents
Steam rising type radial-flow reactor Download PDFInfo
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- CN105833804A CN105833804A CN201610407137.8A CN201610407137A CN105833804A CN 105833804 A CN105833804 A CN 105833804A CN 201610407137 A CN201610407137 A CN 201610407137A CN 105833804 A CN105833804 A CN 105833804A
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- flow
- tube bundle
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- 230000000630 rising effect Effects 0.000 title abstract 4
- 238000006243 chemical reaction Methods 0.000 claims abstract description 137
- 239000003054 catalyst Substances 0.000 claims abstract description 49
- 239000000463 material Substances 0.000 claims abstract description 48
- 239000000498 cooling water Substances 0.000 claims abstract description 25
- 238000009413 insulation Methods 0.000 claims abstract description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 8
- 230000001174 ascending effect Effects 0.000 claims description 32
- 238000001816 cooling Methods 0.000 claims description 15
- 230000008676 import Effects 0.000 claims description 7
- 230000003197 catalytic effect Effects 0.000 claims description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 8
- 229910052799 carbon Inorganic materials 0.000 abstract description 8
- 230000002779 inactivation Effects 0.000 abstract description 7
- 239000006227 byproduct Substances 0.000 abstract description 6
- 230000008901 benefit Effects 0.000 abstract description 4
- 230000000694 effects Effects 0.000 abstract description 4
- 239000000126 substance Substances 0.000 abstract description 4
- 239000003245 coal Substances 0.000 abstract description 2
- 239000012495 reaction gas Substances 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 21
- 239000000919 ceramic Substances 0.000 description 8
- OKKJLVBELUTLKV-UHFFFAOYSA-N methanol Natural products OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 8
- 230000004044 response Effects 0.000 description 7
- 239000003795 chemical substances by application Substances 0.000 description 4
- 238000012546 transfer Methods 0.000 description 4
- 206010020843 Hyperthermia Diseases 0.000 description 3
- 239000000470 constituent Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 230000036031 hyperthermia Effects 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 238000012856 packing Methods 0.000 description 3
- 238000009834 vaporization Methods 0.000 description 3
- 230000008016 vaporization Effects 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 230000006378 damage Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 238000011068 loading method Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 239000011358 absorbing material Substances 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- -1 methanol aromatic hydrocarbons Chemical class 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0207—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly horizontal
- B01J8/0221—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly horizontal in a cylindrical shaped bed
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0285—Heating or cooling the reactor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0292—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds with stationary packing material in the bed, e.g. bricks, wire rings, baffles
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
- B01J2208/00132—Tubes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00743—Feeding or discharging of solids
- B01J2208/00761—Discharging
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Fluid Mechanics (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention provides a steam rising type radial-flow reactor, and relates to the field of petrochemical and coal chemical reactors. The steam rising type radial-flow reactor comprises a reactor shell, a heat exchange tube bundle, a catalyst bed, a flow diversion barrel, a flow confluence barrel, a flow confluence pipe, a reaction material inlet, a water vapor outlet, a reaction material outlet, a cooling water inlet, a catalyst discharge opening and a heat insulation reaction section; the flow diversion barrel, the flow confluence barrel and the flow confluence pipe are sequentially sleeved and communicated; the catalyst bed is arranged in a gap between the flow diversion barrel and the flow confluence barrel; the heat exchange tube bundle passes through the catalyst bed; the bottom of the flow confluence pipe is communicated with the reaction material outlet; the heat insulation reaction section is communicated with the reaction material inlet; a catalyst is arranged in the heat insulation reaction section. According to the steam rising type radial-flow reactor provided by the invention, an effect that reaction gas radially passes through the catalyst bed is achieved; a flow area is large; a pressure drop is low, and temperature distribution is uniform; the local high temperature is avoided; the carbon deposit or inactivation risk of the catalyst is effectively reduced; steam is formed as a byproduct; economic benefits are good.
Description
Technical field
The present invention relates to petrochemical industry and Coal Chemical Industry reactor field, in particular to one
Steam ascending manner radial flow reactors.
Background technology
In recent years, methanol-fueled CLC, carbon monodixe conversion, preparing methane by synthetic gas, ammonia synthesis,
The fields such as methanol-to-olefins, methanol aromatic hydrocarbons, preparing gasoline by methanol are the most noticeable, wherein urge
The research of fluidized bed reactor and the focus improving always this field.Strongly exothermic for fixed bed
Reaction, effectively removes waste heat in course of reaction, maintains reaction temperature stable, it is to avoid to urge
Agent carbon deposit or inactivation, it is ensured that selectivity and the yield of reaction are most important.
According to reaction mass flow direction in the reactor, fixed bed catalytic reactor can divide again
For axial flow reactor and Radial Flow reactor.Owing to current chemical plant installations scale gradually expands
Greatly, traditional axially flowing fixed bed reactors are affected by traffic condition due to diameter so that it is
The space of volume increase is restricted；Additionally, its heat transfer effect also can have much room for improvement.And Radial Flow
Reactor is then owing to loaded catalyst is big, flow process is short, pressure drop is little and becomes reversible exothermic reaction
The preferred reactor type of industrial large-sizedization equipment.But for methanol synthesis reactor, conversion instead
Answering device etc., it is big still to there is thermal discharge in conventional adiabatic reactor radial reactor, the temperature of reactor
Height, wayward, catalyst overtemperature and the cycle of use short problem, add production cost.
Summary of the invention
It is an object of the invention to provide a kind of steam ascending manner radial flow reactors, it can make instead
Answering gas radial through beds, circulation area is big, and pressure drop is low, and uniformity of temperature profile,
Avoid localized hyperthermia, effectively reduce catalyst carbon deposit or inactivation risk, simultaneously byproduct steam, warp
Help profitable.
Embodiments of the invention are achieved in that
A kind of steam ascending manner radial flow reactors, including reactor shell, heat-exchanging tube bundle, urges
Agent bed, shunt cylinder, conflux cylinder and collecting pipe, and the top of reactor shell is provided with reactant
Material import and moisture outlet, the bottom of reactor shell is provided with reacting material outlet, cooling water
Import and catalyst discharge port, moisture outlet connects with the top of heat-exchanging tube bundle, cooling water inlet
Connect with the bottom of heat-exchanging tube bundle；Shunt cylinder is set in the outside of the cylinder that confluxes, the inner chamber of the cylinder that confluxes
With the inner space of shunt cylinder, the jacket casing that confluxes is located at the outside of collecting pipe, the inner chamber of collecting pipe with
Conflux the inner space of cylinder, the inner chamber of shunt cylinder and the inner space of reactor shell, catalyst
Bed be arranged at shunt cylinder and conflux between cylinder gap in, heat-exchanging tube bundle pass catalyst bed
Layer, the bottom of collecting pipe connects with reacting material outlet, and steam ascending manner radial flow reactors is also
Including adiabatic reaction section, adiabatic reaction section connects with reacting material inlet, sets in adiabatic reaction section
It is equipped with catalyst.
Further, in a preferred embodiment of the invention, above-mentioned heat-exchanging tube bundle is located on and confluxes
The outside of cylinder, adiabatic reaction section includes internal layer adiabatic reaction section and secondary insulation conversion zone, heat exchange
Beds between tube bank and shunt cylinder forms secondary insulation conversion zone, heat-exchanging tube bundle and remittance
Beds between flow cartridge forms internal layer adiabatic reaction section.
Further, in a preferred embodiment of the invention, the footpath of above-mentioned secondary insulation conversion zone
To thickness be shunt cylinder to the cylinder that confluxes radial distance 5%～40%；Internal layer adiabatic reaction section
Radial thickness is shunt cylinder to the 2%～35% of the radial distance of the cylinder that confluxes.
Further, in a preferred embodiment of the invention, above-mentioned adiabatic reaction section is arranged on instead
In answering device housing, adiabatic reaction section is positioned at the lower section of reacting material inlet, and is positioned at shunt cylinder
Top.
Further, in a preferred embodiment of the invention, above-mentioned steam ascending manner radial flow is anti-
Answering device also to include adiabatic reactor, it is external that adiabatic reactor is positioned at reactor enclosure, adiabatic reaction section
Being arranged in adiabatic reactor, adiabatic reactor is provided with pre-reaction import and pre-reaction outlet,
Pre-reaction outlet connects with reacting material inlet.
Further, in a preferred embodiment of the invention, the top of above-mentioned collecting pipe seals,
Collecting pipe is provided with multiple first through hole, and the inner chamber of the inner chamber of collecting pipe and the cylinder that confluxes is by first
Through hole connects；Being provided with multiple third through-hole on the barrel of shunt cylinder, the inner chamber of shunt cylinder is with anti-
The inner chamber answering device housing is connected by third through-hole, between existing between shunt cylinder and reactor shell
Gap, forms split channel.
Further, in a preferred embodiment of the invention, the barrel of the above-mentioned cylinder that confluxes is provided with
Multiple second through holes, the inner chamber of the cylinder that confluxes is connected by the second through hole with the inner chamber of shunt cylinder.
Further, in a preferred embodiment of the invention, the above-mentioned cylinder that confluxes is made up of silk screen.
Further, in a preferred embodiment of the invention, above-mentioned heat-exchanging tube bundle includes that many are changed
Heat pipe, Vapor Sink house steward, cooling supply mains, upper perforated plate and lower perforated plate, the top of Vapor Sink house steward
End connects with moisture outlet, and the bottom of Vapor Sink house steward is connected with upper perforated plate, cooling supply mains's
Top is connected with lower perforated plate, and the bottom of cooling supply mains connects with cooling water inlet, and heat exchanger tube leads to
Cross upper perforated plate and lower perforated plate is fixed in reactor enclosure body.
Further, in a preferred embodiment of the invention, above-mentioned Vapor Sink house steward, cooling water
The quantity of house steward, moisture outlet, cooling water inlet, upper perforated plate and lower perforated plate is 1～6.
The embodiment of the present invention provides the benefit that: by arrange in reactor enclosure body shunt cylinder,
Conflux cylinder and collecting pipe, shunt cylinder, confluxes cylinder and collecting pipe is sequentially communicated, and catalyst bed
Layer be arranged at shunt cylinder and conflux between cylinder, it is achieved reacting gas radial through beds,
Circulation area is big, and system pressure drop is low, the steam ascending manner radial flow reactors that the present invention provides
Pressure drop is only the 10%～50% of axial flow reactor pressure drop.Cooling water flows in tube side, logical
Overflash removes the heat that reaction produces, whole heat-exchanging tube bundle uniformity of temperature profile, it is to avoid local
High temperature, effectively reduces catalyst carbon deposit or inactivation risk, greatly reduces heat-exchanging tube bundle to material
The requirement of high temperature heat-resistant, effectively reduces equipment investment.By-product high pressure or middle pressure steam simultaneously,
Good in economic efficiency.By controlling steam outlet pressure, the reaction temperature of isothermal section can be controlled,
Whole response system temperature flexible adjustment, effectively.The most in the present embodiment, by arranging absolutely
Thermal response section, makes reacting gas carry out pre-reaction, reacting gas elder generation and urging in adiabatic reaction section
Agent carries out pre-reaction, and adiabatic reaction section can eliminate part harmful constituent in reaction mass, and
Reacting gas is preheated, makes reacting gas reach ideal feed state.
Accompanying drawing explanation
In order to be illustrated more clearly that the technical scheme of the embodiment of the present invention, below will be in embodiment
The required accompanying drawing used is briefly described, it will be appreciated that the following drawings illustrate only this
Some bright embodiment, is therefore not construed as the restriction to scope, common for this area
From the point of view of technical staff, on the premise of not paying creative work, it is also possible to according to these accompanying drawings
Obtain other relevant accompanying drawings.
The knot of the steam ascending manner radial flow reactors that Fig. 1 provides for first embodiment of the invention
Structure schematic diagram；
The knot of the steam ascending manner radial flow reactors that Fig. 2 provides for second embodiment of the invention
Structure schematic diagram；
The knot of the steam ascending manner radial flow reactors that Fig. 3 provides for third embodiment of the invention
Structure schematic diagram.
In figure:
Steam ascending manner radial flow reactors 100,200,300；
Reactor shell 110,210；Top end socket 111；Middle cylinder 112；Bottom head
113；Reacting material inlet 114；Reacting material outlet 115；Cooling water inlet 116；Steam
Outlet 117；Catalyst discharge port 118；
Heat-exchanging tube bundle 120；Heat exchanger tube 121；Vapor Sink house steward 122；Cooling supply mains 123；
Upper perforated plate 124；Lower perforated plate 125；
Beds 130；
Shunt cylinder 141；Conflux cylinder 142,242；Collecting pipe 143；First through hole 144；The
Two through holes 145；Third through-hole 146；
Air distributor 150；
Inert ceramic balls layer 160；
Shunt cylinder cover plate 170；
Heat-exchanging tube bundle support member 180；
Adiabatic reactor 290；Adiabatic reaction section 191,291,391；Secondary insulation conversion zone
191a；Internal layer adiabatic reaction section 191b；Pre-reaction import 292；Pre-reaction outlet 293.
Detailed description of the invention
For making the purpose of the embodiment of the present invention, technical scheme and advantage clearer, below will knot
Close the accompanying drawing in the embodiment of the present invention, the technical scheme in the embodiment of the present invention is carried out clear,
Be fully described by, it is clear that described embodiment be a part of embodiment of the present invention rather than
Whole embodiments.Generally herein described in accompanying drawing and the assembly of the embodiment of the present invention that illustrates
Can arrange with various different configurations and design.
Therefore, detailed description not purport to the embodiments of the invention provided in the accompanying drawings below
Limit the scope of claimed invention, but be merely representative of the selected enforcement of the present invention
Example.Based on the embodiment in the present invention, those of ordinary skill in the art are not making creativeness
The every other embodiment obtained under work premise, broadly falls into the scope of protection of the invention.
It should also be noted that similar label and letter expression similar terms in following accompanying drawing, therefore,
The most a certain Xiang Yi accompanying drawing is defined, then need not it is carried out in accompanying drawing subsequently
Definition and explanation further.
In describing the invention, it should be noted that term " " center ", " on ", D score,
Orientation or the position relationship of the instruction such as " level ", " interior ", " outward " are based on side shown in the drawings
Position or position relationship, or when this invention product uses, the orientation usually put or position are closed
System, or the orientation that usually understands of those skilled in the art or position relationship, merely to just
Describe in the description present invention and simplification rather than indicate or imply that the device of indication or element are necessary
There is specific orientation, with specific azimuth configuration and operation, therefore it is not intended that to this
Bright restriction.Describe additionally, term " first ", " second ", " the 3rd " etc. are only used for distinguishing,
And it is not intended that indicate or hint relative importance.
In describing the invention, in addition it is also necessary to explanation, unless otherwise clear and definite regulation and limit
Fixed, term " is arranged ", " installation ", " connection " should be interpreted broadly, for example, it may be consolidate
Fixed connection, it is also possible to be to removably connect, or be integrally connected；Can be to be joined directly together, also
Can be indirectly connected to by intermediary, it is also possible to be the connection of two element internals.For this
For the those of ordinary skill in field, above-mentioned term can be understood in the present invention with concrete condition
Concrete meaning.
First embodiment
Refer to Fig. 1, the present embodiment provides a kind of steam ascending manner radial flow reactors 100,
It include reactor shell 110, heat-exchanging tube bundle 120, beds 130, shunt cylinder 141,
Conflux cylinder 142 and collecting pipe 143, heat-exchanging tube bundle 120, beds 130, shunt cylinder
141, conflux cylinder 142 and collecting pipe 143 is separately positioned on the inside of reactor shell 110.
In the present embodiment, reactor shell 110 includes top end socket 111, middle cylinder 112
With bottom head 113.Top end socket 111 is provided with reacting material inlet 114 and moisture outlet
117, bottom head 113 is provided with reacting material outlet 115, cooling water inlet 116 and urges
Agent discharge port 118.Wherein, moisture outlet 117 connects with the top of hot heat-exchanging tube bundle 120,
Cooling water inlet 116 connects with the bottom of heat-exchanging tube bundle 120.
Reaction mass enters in reactor shell 110 from reacting material inlet 114 and reacts
After, discharge from reacting material outlet 115；Cooling water enters from cooling water inlet 116, passes through
Heat-exchanging tube bundle 120, cooling water is reacted by reaction mass in vaporization absorption reactor shell 110
After the heat discharged, discharge from moisture outlet 117.In the present embodiment, reacting material inlet
114 can be used as catalyst filling mouth, for loading catalyst, shape in reactor shell 110
Become beds 130, it is not necessary to separately set catalyst filling mouth, save equipment cost.In filling
During catalyst, catalyst is put in reactor shell 110 from reacting material inlet 114, instead
After a period of time, then catalyst should be unloaded from the catalyst discharge port 118 of reactor shell 110
Going out, the handling of catalyst are very convenient, quick.Meanwhile, reacting material inlet 114 is also
Can be used as manhole to use, conveniently inside reactor overhauled and clear up.The embodiment of the present invention
In, Catalyst packing is outside tube bank, and cooling water, at tube side flow, is removed reaction by vaporization and produced
Raw heat, whole heat-exchanging tube bundle 120 uniformity of temperature profile, it is to avoid localized hyperthermia, reduces
Catalyst carbon deposit or inactivation risk, by-product high pressure or middle pressure steam, good in economic efficiency simultaneously.
The cooling medium that cooling water inlet 116 is passed through is the aqueous water of saturation.Due to saturated
The water of state is temperature-resistant in vaporescence, and the temperature in whole heat-exchanging tube bundle 120 keeps not
Become, the heat that heat-exchanging tube bundle 120 is released when absorbing material reaction in reactor shell 110, make
Obtain internal aqueous water and be constantly evaporated to steam, form gas-vapor mix, constantly from top end socket
The moisture outlet 117 of 111 is discharged, by controlling the outlet pressure of moisture outlet 117, permissible
Control the reaction temperature in reactor shell 110 so that the temperature of whole response system can spirit
Live and be effectively adjusted.
Specifically, seeing Fig. 1, heat-exchanging tube bundle 120 includes many heat exchanger tubes 121, Vapor Sinks
House steward 122 and cooling supply mains 123, wherein, the two ends of Vapor Sink house steward 122 respectively with change
The top of heat pipe 121 connects with moisture outlet 117, cooling supply mains 123 two ends respectively with
The bottom of heat exchanger tube 121 connects with cooling water inlet 116, and cooling water is from cooling water inlet 116
Enter in cooling supply mains 123, be then tapped off in many heat exchanger tubes 121, increase heat-transfer surface
Long-pending, fully reaction liberated heat in reactor shell 110 is absorbed, converge the most again
Always discharge in Vapor Sink house steward 122.Meanwhile, in the present embodiment, also at shunt cylinder 141
And conflux and between cylinder 142, be provided with heat-exchanging tube bundle support member 180, heat-exchanging tube bundle support member 180
It is connected with heat-exchanging tube bundle 120, and can heat exchanging tube bank 120 play a supporting role, it is to avoid because of
Heat-exchanging tube bundle 120 shakes and damages beds 130.
The upper perforated plate for fixing heat exchanger tube 121 top it is provided with in Vapor Sink house steward 122
124, it is provided with the lower perforated plate for fixing heat exchanger tube 121 bottom in cooling supply mains 123
125, by upper perforated plate 124 and the setting of lower perforated plate 125 so that heat exchanger tube 121 can be solid
In reactor shell 110, simultaneously by outside the tube side steam in reactor shell 110 and pipe
Reaction mass is effectively isolated.
The cooling water inlet 116 that is sequentially communicated, cooling supply mains 123, lower perforated plate 125, many
Root heat exchanger tube 121, upper perforated plate 124, Vapor Sink house steward 122 and moisture outlet 117 form one
Group heat-exchanging tube bundle 120, quantity is 1～6 group.In the present embodiment, preferably heat-exchanging tube bundle 120 is
Four groups, and be symmetrical arranged.Specifically, in the present embodiment, moisture outlet 117 is four, and
Four moisture outlet 117 are symmetrical arranged, and in like manner, cooling water inlet 116 is also four, and point
Not corresponding with the position of four moisture outlet 117.Correspondingly, in the present embodiment, steam collects
Pipe 122, cooling supply mains 123, upper perforated plate 124 and lower perforated plate 125 also correspond to four.
In the present embodiment, heat exchanger tube 121 is disposed through shunt cylinder 141 and confluxes between cylinder 142
Beds 130, and symmetrical so that in whole reactor, heat exchange is uniform, and reaction
Material flows through the resistance drop of beds 130 and is evenly distributed, beneficially the heat transfer in reactor
With mass transfer.Certainly, in other embodiments, can according to the size of reactor shell 110, or
The demand of heat exchange area, the group number of heat exchanging tube bank 120 is adjusted correspondingly.
Seeing Fig. 1, in the embodiment of the present invention, shunt cylinder 141, conflux cylinder 142 and collecting pipe
143 are tube structure, are arranged in reactor shell 110.Wherein, shunt cylinder 141 overlaps
Being located at the outside of the cylinder 142 that confluxes, the cylinder 142 that confluxes is set in the outside of collecting pipe 143, shunting
The inner space of inner chamber and the reactor shell 110 of cylinder 141, the inner chamber of the cylinder 142 that confluxes with point
The inner space of flow cartridge 141, the inner space of the inner chamber of collecting pipe 143 and the cylinder 142 that confluxes,
Beds 130 is arranged in shunt cylinder 141 and the gap confluxed between cylinder 142, heat exchange
Tube bank 120 is through beds 130, the bottom of collecting pipe 143 and reacting material outlet 115
Connection.
Specifically, the top of collecting pipe 143 seals, and is provided with on the tube wall of collecting pipe 143
Multiple first through holes 144, the inner chamber of the inner chamber of collecting pipe 143 and the cylinder 142 that confluxes is by first
Through hole 144 connects, same, is provided with multiple second through hole on the barrel of cylinder 142 that confluxes
145, the barrel of shunt cylinder 141 is provided with multiple third through-hole 146, conflux cylinder 142
The inner chamber of inner chamber and shunt cylinder 141 connected by the second through hole 145, shunt cylinder 141 interior
Chamber is connected by third through-hole 146 with the inner chamber of reactor shell 110.Shunt cylinder 141 is with anti-
Answering and there is gap between device housing 110, this gap forms reaction mass split channel.Reaction gas
Body enters reactor shell 110 from reacting material inlet 114, shunts through split channel,
Reacting gas after shunting enters in shunt cylinder 141 from the third through-hole 146 of shunt cylinder 141,
Contact with the beds 130 in shunt cylinder 141 and react, after reaction, by converging
The second through hole 145 in flow cartridge 142 and the first through hole 144 on collecting pipe 143 enter and conflux
Pipe 143, finally discharges from reacting material outlet 115.
In the present embodiment, by shunt cylinder 141, conflux cylinder 142 and collecting pipe 143 ingenious
Design, it is achieved reacting gas is radial through beds 130, and circulation area is big, system pressure
Reducing, the pressure drop of the steam ascending manner radial flow reactors 100 that the present invention provides is only axially stream
The 10%～50% of reactor pressure decrease.Meanwhile, conflux cylinder 142 and collecting pipe 143 sheathed, can
It is prevented effectively from being brought into collecting pipe 143 because of the catalyst in beds 130 by air-flow and causes
System jams and catalyst loss.Additionally, confluxed cylinder 142 and collecting pipe 143 by setting
Can suitably increase fluid and flow through the resistance drop of the facility that confluxes ratio in system drag overall is dropped, make
Obtain air-flow to be more evenly distributed when Radial Flow.
Specifically, in the present embodiment, first through hole the 144, second through hole 145 and third through-hole
146 it is distributed evenly in collecting pipe 143 respectively, confluxes on cylinder 142 and shunt cylinder 141.The
The diameter of one through hole the 144, second through hole 145 and third through-hole 146 is 1～8mm, should
Aperture can make the circulation of reacting gas smooth and easy, can be effectively prevented again catalyst and be brought into instead by air-flow
Answer material outlet 115.In the present embodiment, collecting pipe 143, the cylinder 142 that confluxes top the closeest
Envelope is arranged, additionally, be provided with shunt cylinder cover plate 170 at shunt cylinder top, it is to avoid reacting gas
Enter from the top of shunt cylinder 141, cause the short circuit of reaction mass runner.By the sealing at top
Arrange, define that reacting gas can only radially flow, make reacting gas and beds
The contact of 130 is more abundant, reacts more complete.And in the embodiment of the present invention, shunt cylinder cover plate
170 are spliced by multiple dismountable plates, conveniently when Catalyst packing to shunt cylinder cover plate
170 dismantle.
Further, in the present embodiment, steam ascending manner radial flow reactors 100 also includes absolutely
Thermal response section 191, adiabatic reaction section 191 connects with reacting material inlet 114, adiabatic reaction
It is provided with catalyst in section 191.The reaction mass first catalyst in adiabatic reaction section 191
Catalytic action under carry out pre-reaction, adiabatic reaction section 191 can eliminate part in reaction mass
Harmful constituent, and utilize pre-reaction heat that reacting gas is preheated, make reacting gas reach relatively
For preferable feed state.
Adiabatic reaction section 191 can be arranged on the inside of reactor shell 110, it is also possible to arranges
Outside in reactor shell 110.
Adiabatic reaction section 191 is preferably arranged on the inside of reactor shell 110 by the present embodiment,
Specifically, adiabatic reaction section 191 includes secondary insulation conversion zone 191a and internal layer adiabatic reaction
Section 191b, the heat-exchanging tube bundle 121 in the present embodiment, it is evenly distributed in and confluxes outside cylinder 142
Side, and arrange ringwise, it is filled with in the gap between heat-exchanging tube bundle 120 and shunt cylinder 141
Beds 130, this partial catalyst bed 130 is not owing to setting heat exchanger tube 121, and position
In heat-exchanging tube bundle 120 near the side of shunt cylinder 141, the therefore beds quilt of this part
It is considered as secondary insulation conversion zone 191a, and heat-exchanging tube bundle 120 and between confluxing between cylinder 142
Being also filled with beds 130 in gap, this partial catalyst bed 130 is not owing to setting heat exchange
Pipe 121, and be positioned at heat-exchanging tube bundle 120 side near the cylinder 142 that confluxes, therefore this part
Beds is considered internal layer adiabatic reaction section 191b, and internal layer adiabatic reaction section 191b and
Owing to being provided with heat-exchanging tube bundle 120 between secondary insulation conversion zone 191a, pass through heat-exchanging tube bundle
Interior cooling water absorbs heat of reaction fully, so that this part bed can keep reaction temperature
Stablizing of degree, therefore, this part bed is considered isothermal reaction section.
In the present embodiment, the radial thickness of secondary insulation conversion zone 191a is that shunt cylinder 141 arrives
Conflux cylinder 142 radial distance 5%～40%, the radial direction of internal layer adiabatic reaction section 191b is thick
The 2%～35% of the radial distance that degree is shunt cylinder 141 to the cylinder 142 that confluxes.
Reaction mass, after the reacting material inlet 114 of reactor shell 110 enters, first exists
Carry out pre-reaction under the catalyst action of secondary insulation conversion zone 191a, utilize secondary insulation anti-
Material is preheated by the heat that the section of answering 191a pre-reaction is released so that it is temperature reaches optimum response
Temperature, effectively eliminates the harmful substance in raw material by pre-reaction simultaneously.Material after pre-reaction
Entering isothermal reaction section, isothermal reaction section utilizes the water vapor in heat-exchanging tube bundle 120, removes anti-
Answer liberated heat, and byproduct steam, make reaction condition close to isothermal operation, be prevented effectively from
The problem such as catalyst carbon deposit that high temperature causes or inactivation.After isothermal reaction section is reacted, big portion
Reactive material is divided to participate in reaction, less at the response magnitude of internal layer adiabatic reaction section 191b,
Temperature rise is relatively low, therefore can be without heat exchange.The setting of internal layer adiabatic reaction section 191b, adds
The total conversion of reaction, simultaneously because be not provided with heat-exchanging tube bundle in internal layer adiabatic reaction section 191b
120, unit volume inner catalyst loadings is big, can effectively reduce the volume of reactor.
See Fig. 1, in the present embodiment, also set in the bottom head 113 of reactor shell 110
It is equipped with inert ceramic balls layer 160.This inert ceramic balls layer 160 is positioned at the lower section of beds 130,
When carrying out catalyst filling, first inert ceramic balls is loaded the bottom head into reactor shell 110
In 113, form inert ceramic balls layer 160, then catalyst is deposited in inert ceramic balls layer 160
Above.Well beds 130 can be played by arranging inert ceramic balls layer 160
Support effect.
Seeing Fig. 1, further, the lower section of reacting material inlet 114 is provided with air flow method
Device 150, the gas material of reaction can be at air flow method after reacting material inlet 114 enters
Shunt under the effect of device 150, contact with catalyst more fully, it is to avoid bigger stream
The air-flow of the speed destruction to beds 130.
Second embodiment
Seeing Fig. 2, the present embodiment provides a kind of steam ascending manner radial flow reactors 200, its
It is roughly the same with the structure of the steam ascending manner radial flow reactors 100 that first embodiment provides,
The adiabatic reaction section 271 that the difference of the two is in the present embodiment is arranged at reactor shell 210
Outside, and the cylinder 242 that confluxes in the present embodiment uses silk screen to make.
In the present embodiment, steam ascending manner radial flow reactors 200 includes reactor shell 210
With adiabatic reactor 290, this adiabatic reactor 290 connects with reactor shell 210.
Adiabatic reactor 290 be provided with pre-reaction import 292, adiabatic reaction section 291 and pre-instead
293 should be exported, pre-reaction outlet 293 and the reacting material inlet 114 of reactor shell 210
Connection, this adiabatic reactor 290 is positioned at the outside of reactor shell 210, and both are split
Formula structure, reacting gas is entered in adiabatic reactor 290 by pre-reaction import 292, and
Adiabatic reaction section 291 carries out pre-reaction, after pre-reaction, anti-by pre-reaction outlet 293 entrance
Answer material inlet 114, thus react in reactor shell 210.
The present embodiment, can be more by reacting gas being carried out pre-reaction outside reactor shell 210
Good detection and the pre-reaction situation of control reaction mass, additionally, the catalyst dress of pre-reaction section
Unload more convenient.
Meanwhile, in the present embodiment, the cylinder 242 that confluxes uses silk screen to make, and at the cylinder 242 that confluxes
And load inert ceramic balls layer between collecting pipe 143, silk screen is effectively supported.The net of silk screen
Shape structure can not only avoid catalyst to enter in collecting pipe 143, also ensures that good simultaneously
Air penetrability.In the present embodiment, by arranging the cylinder 242 that confluxes that silk screen is made, it is not necessary to use and open
The tube structure in hole, making is more prone to, and equipment cost is lower.
3rd embodiment
Seeing Fig. 3, the present embodiment provides a kind of steam ascending manner radial flow reactors 300, its
It is roughly the same with the structure of the steam ascending manner radial flow reactors 100 that first embodiment provides,
The adiabatic reaction section 391 that the difference of the two is in the present embodiment is arranged at reacting material inlet
The lower section of 114, and it is positioned at the top of shunt cylinder 141.
Adiabatic reaction section 391 be positioned at the lower section of reacting material inlet 114, shunt cylinder 141 upper
Side, and contact with Vapor Sink house steward 122.Due to changing in this section of beds unit volume
Hot side is long-pending less, is accordingly regarded as adiabatic reaction section.Reacting gas is from reacting material inlet 114
Enter in reactor shell 110, then carry out under the catalyst action of adiabatic reaction section 391
Pre-reaction, the reacting gas after pre-reaction enters split channel, then through third through-hole 146
Entering beds 130 and carry out catalytic reaction, reacted material, by the cylinder 142 that confluxes
On the second through hole 145 and the first through hole 144 on collecting pipe 143 enter collecting pipe 143
In, and discharge from reacting material outlet 115.
In sum, the present invention by arranging shunt cylinder 141, conflux cylinder 142 and collecting pipe 143,
Shunt cylinder 141, conflux cylinder 142 and collecting pipe 143 is sequentially communicated, and beds 130
It is arranged at shunt cylinder 141 and confluxes between cylinder 142, it is achieved reacting gas is radial through catalyst
Bed 130, circulation area is big, and system is forced down.The steam ascending manner radial flow that the present invention provides
The pressure drop of reactor 100 is only the 10～50% of axial flow reactor pressure drop.Catalyst packing in
Outside tube bank, cooling water flow in tube side, is removed the heat of reaction generation by vaporization, whole changes
Heat pipe bundle 120 uniformity of temperature profile, it is to avoid localized hyperthermia, effectively reduce catalyst carbon deposit or
Inactivation risk, greatly reduces the heat-exchanging tube bundle 120 requirement to material high temperature heat-resistant, effectively drops
Low equipment investment.By-product high pressure or middle pressure steam, good in economic efficiency simultaneously.By controlling water
Vapor outlet port pressure, can control the reaction temperature of isothermal section, the regulation spirit of whole response system temperature
Live, effectively.Adiabatic reaction section 191 is set, reaction mass is carried out pre-reaction, eliminate reaction
Part harmful constituent in material, and reaction mass is preheated so that it is reach ideal
Feed state.Therefore the present invention has reaction pressure reduction, the advantage such as reduced investment, flexible adjustment.
The foregoing is only the preferred embodiments of the present invention, be not limited to the present invention,
For a person skilled in the art, the present invention can have various modifications and variations.All at this
Within the spirit of invention and principle, any modification, equivalent substitution and improvement etc. made, all should
Within being included in protection scope of the present invention.
Claims (10)
1. a steam ascending manner radial flow reactors, it is characterised in that include reactor
Housing, heat-exchanging tube bundle, beds, shunt cylinder, conflux cylinder and collecting pipe, described reaction
The top of device housing is provided with reacting material inlet and moisture outlet, the bottom of described reactor shell
Be provided with reacting material outlet, cooling water inlet and catalyst discharge port, described moisture outlet with
The top connection of described heat-exchanging tube bundle, described cooling water inlet connects with the bottom of described heat-exchanging tube bundle
Logical；Described shunt cylinder confluxes the outside of cylinder described in being set in, described in conflux the inner chamber of cylinder with described
The inner space of shunt cylinder, described in the jacket casing that confluxes be located at the outside of described collecting pipe, described in conflux
The inner chamber of pipe and the inner space of the described cylinder that confluxes, the inner chamber of described shunt cylinder and described reactor
The inner space of housing, described beds be arranged at described shunt cylinder with described conflux cylinder it
Between gap in, described heat-exchanging tube bundle pass described beds, the bottom of described collecting pipe
Connecting with described reacting material outlet, described steam ascending manner radial flow reactors also includes thermal insulation
Conversion zone, described adiabatic reaction section connects with described reacting material inlet, described adiabatic reaction section
Inside it is provided with catalyst.
Steam ascending manner radial flow reactors the most according to claim 1, its feature
Be, described heat-exchanging tube bundle be located on described in conflux the outside of cylinder, described adiabatic reaction section includes
Internal layer adiabatic reaction section and secondary insulation conversion zone, between described heat-exchanging tube bundle and described shunt cylinder
Described beds form described secondary insulation conversion zone, described heat-exchanging tube bundle and described remittance
Described beds between flow cartridge forms described internal layer adiabatic reaction section.
Steam ascending manner radial flow reactors the most according to claim 2, its feature
Be, the radial thickness of described secondary insulation conversion zone be described shunt cylinder to described in conflux cylinder
The 5%～40% of radial distance；The radial thickness of described internal layer adiabatic reaction section is described shunt cylinder
Conflux described in cylinder radial distance 2%～35%.
Steam ascending manner radial flow reactors the most according to claim 1, its feature
Being, described adiabatic reaction section is arranged in described reactor enclosure body, described adiabatic reaction section
In the lower section of described reacting material inlet, and it is positioned at the top of described shunt cylinder.
Steam ascending manner radial flow reactors the most according to claim 1, its feature
Being, described steam ascending manner radial flow reactors also includes adiabatic reactor, and described thermal insulation is anti-
Answering device to be positioned at described reactor enclosure external, described adiabatic reaction section is arranged on described adiabatic reactor
In, described adiabatic reactor is provided with pre-reaction import and pre-reaction outlet, and described pre-reaction goes out
Mouth connects with described reacting material inlet.
Steam ascending manner radial flow reactors the most according to claim 1, its feature
Being, the top of described collecting pipe seals, and described collecting pipe is provided with multiple first through hole, institute
The inner chamber stating collecting pipe is connected by described first through hole with the inner chamber of the described cylinder that confluxes；Described point
Multiple third through-hole it is provided with, the inner chamber of described shunt cylinder and described reactor on the barrel of flow cartridge
The inner chamber of housing is connected by described third through-hole, described shunt cylinder and described reactor shell it
Between there is gap, form split channel.
Steam ascending manner radial flow reactors the most according to claim 1, its feature
Be, described in the conflux barrel of cylinder be provided with multiple second through hole, described in conflux cylinder inner chamber and
The inner chamber of described shunt cylinder is connected by described second through hole.
Steam ascending manner radial flow reactors the most according to claim 1, its feature
Be, described in the cylinder that confluxes be made up of silk screen.
Steam ascending manner catalytic bed reactor the most according to claim 1, its feature
Be, described heat-exchanging tube bundle include many heat exchanger tubes, Vapor Sink house steward, cooling supply mains, on
Tube sheet and lower perforated plate, the top of described Vapor Sink house steward connects with described moisture outlet, described water
The bottom of vapour gathering tube is connected with described upper perforated plate, described cooling supply mains top with described under
Tube sheet connects, and the bottom of described cooling supply mains connects with described cooling water inlet, described heat exchange
Pipe is fixed in described reactor enclosure body by described upper perforated plate and described lower perforated plate.
Steam ascending manner catalytic bed reactor the most according to claim 9, its feature
It is, described Vapor Sink house steward, described cooling supply mains, described moisture outlet, described cooling
The quantity of water inlet, described upper perforated plate and described lower perforated plate is 1～6.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106763910A (en) * | 2017-01-22 | 2017-05-31 | 成都赛普瑞兴科技有限公司 | A kind of whirligig and gas fractionation unit |
| CN108722339A (en) * | 2018-06-11 | 2018-11-02 | 湖南安淳高新技术有限公司 | Radial air cooling reactor |
| CN109395668A (en) * | 2017-08-18 | 2019-03-01 | 上海浦景化工技术股份有限公司 | A kind of coupled reactor for oxalic acid Arrcostab hydrogenation synthesizing of ethylene glycol |
| CN111905657A (en) * | 2019-05-07 | 2020-11-10 | 上海浦景化工技术股份有限公司 | Reactor for preparing ethylene glycol from large-scale synthesis gas |
| CN112191197A (en) * | 2020-10-20 | 2021-01-08 | 南京聚拓化工科技有限公司 | Composite ethylene glycol hydrogenation reactor and ethylene glycol hydrogenation process |
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| CN104096514A (en) * | 2013-04-09 | 2014-10-15 | 上海国际化建工程咨询公司 | Isothermal fixed bed reactor loading catalyst among heat exchange tubes |
| CN205700479U (en) * | 2016-06-08 | 2016-11-23 | 成都赛普瑞兴科技有限公司 | Steam ascending manner radial flow reactors |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104096514A (en) * | 2013-04-09 | 2014-10-15 | 上海国际化建工程咨询公司 | Isothermal fixed bed reactor loading catalyst among heat exchange tubes |
| CN205700479U (en) * | 2016-06-08 | 2016-11-23 | 成都赛普瑞兴科技有限公司 | Steam ascending manner radial flow reactors |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106763910A (en) * | 2017-01-22 | 2017-05-31 | 成都赛普瑞兴科技有限公司 | A kind of whirligig and gas fractionation unit |
| CN106763910B (en) * | 2017-01-22 | 2023-08-11 | 成都赛普瑞兴科技有限公司 | Rotating device and gas separation device |
| CN109395668A (en) * | 2017-08-18 | 2019-03-01 | 上海浦景化工技术股份有限公司 | A kind of coupled reactor for oxalic acid Arrcostab hydrogenation synthesizing of ethylene glycol |
| CN108722339A (en) * | 2018-06-11 | 2018-11-02 | 湖南安淳高新技术有限公司 | Radial air cooling reactor |
| CN111905657A (en) * | 2019-05-07 | 2020-11-10 | 上海浦景化工技术股份有限公司 | Reactor for preparing ethylene glycol from large-scale synthesis gas |
| CN112191197A (en) * | 2020-10-20 | 2021-01-08 | 南京聚拓化工科技有限公司 | Composite ethylene glycol hydrogenation reactor and ethylene glycol hydrogenation process |
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|---|---|
| CN105833804B (en) | 2018-12-28 |
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